CN112226240B - Device and method for preparing semi-coke from coal - Google Patents
Device and method for preparing semi-coke from coal Download PDFInfo
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- CN112226240B CN112226240B CN202010992832.1A CN202010992832A CN112226240B CN 112226240 B CN112226240 B CN 112226240B CN 202010992832 A CN202010992832 A CN 202010992832A CN 112226240 B CN112226240 B CN 112226240B
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
- C10B53/04—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of powdered coal
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
Abstract
The invention provides a device and a method for preparing semi-coke from coal. The three units are arranged in one device and are relatively independent in operation, and the device is simple in structure, small in occupied area, strong in adjustability, high in comprehensive energy efficiency and stable in operation. The method utilizes the pulverized coal gasification semicoke as a circulating heat carrier for pulverized coal gasification, the pulverized coal gasification gas as a heat carrier for preparing the semi-coke by pyrolysis of lump coal, and the lump coal pyrolysis chamber also serves as a movable particle dust removal chamber for preliminarily removing dust from the pulverized coal gasification gas, and then utilizes the gas dust removal chamber for carrying out in-situ thermal dust removal on the gasification and pyrolysis gas, so that the treatment of full-particle-size coal, the self-heating balance of energy and the self-purification of gas are realized, and the quality of the semi-coke, the byproduct gas and tar is high.
Description
Technical Field
The invention belongs to the technical field of energy chemical industry, and relates to a heat treatment device and a heat treatment method, in particular to a device and a method for preparing semi-coke from coal.
Background
Semi coke prepared by high-volatile bituminous coal through a medium-low temperature pyrolysis technology, has the characteristics of high fixed carbon, high specific resistance, high chemical activity, low ash, low aluminum, low sulfur and the like, is usually granular, and is widely used as a reducing agent for producing ferroalloy and calcium carbide, a raw material for blast furnace injection and industrial and civil clean fuel. The industrial semi-coke production technology mainly adopts an internal heating type vertical furnace which takes flue gas as a gas heat carrier, such as an SJ furnace, an SH furnace and a GF furnace, but the particle size range of the coal processed by the furnace types is limited at present, and lump coal is mainly adopted, so that a large amount of fine coal resources in mechanized mining are wasted. Meanwhile, the smoke contains a large amount of N2And CO2Resulting in low gas calorific value.
Aiming at the problem of low utilization rate of raw material coal in the existing semi-coke production technology, various semi-coke preparation technologies capable of simultaneously utilizing lump coal and pulverized coal are developed. Patent CN201510209036.5 discloses a lump coal and pulverized coal combined drying and dry distillation method and device, and the technical scheme is as follows: screening raw coal with the particle size of less than 100mm into lump coal with the particle size of more than or equal to 10mm and pulverized coal with the particle size of less than 10mm, and then respectively drying and dry distilling; performing dry distillation on the lump coal dried by the flue gas in a dry distillation chamber provided with a plurality of venturi tube burners by taking partial combustion heat of air and the lump coal as a main heat source and taking pulverized coal pyrolysis gas as a supplementary heat source, mixing the generated coal gas with the coal gas generated by the pulverized coal dry distillation, cooling and separating to obtain coal gas and tar, and taking the generated semicoke as a heat carrier for pulverized coal pyrolysis; the pulverized coal dried by the flue gas is mixed with high-temperature semicoke generated by pyrolysis of lump coal in a double-helix mixing pyrolyzer, and is subjected to destructive distillation after being indirectly contacted with combustion flue gas of an external fuel for heat compensation, and the generated mixed semicoke is cooled and quenched to be output as a product. The method has the following disadvantages: large-particle semicoke is used as a heat carrier for pulverized coal dry distillation, and the heat transfer efficiency is low; external fuel combustion heat supplement is needed during pulverized coal pyrolysis, and the comprehensive energy efficiency of the system is low; the air combustion supplies heat for the pyrolysis of lump coal, so that the quality of coal gas generated by pyrolysis is low; pyrolysis gas that fine coal produced gets into the cloth gas pocket through external gas distribution channel and for lump coal pyrolysis concurrent heating, and the pyrolysis coal gas of fine coal and lump coal directly cools off the separation through removing dust, because the change tar and the dust of temperature block up the pipeline easily in the transportation, the unable steady operation of device.
Patent CN201310109786.6 discloses a system and method for omnibearing coal quality-based utilization and poly-generation, which comprises a coal preparation system, a lump coal pyrolysis system, a granular coal pyrolysis system, a crude gas treatment system and a gasification system. The method comprises the following steps of (1) dividing raw material coal into lump coal and granular coal by using a coal preparation system, pyrolyzing the lump coal by using gasified coal gas generated by a gasification system as a heat carrier, using generated pyrolysis oil gas as the heat carrier of a granular coal pyrolysis system, and outputting pyrolysis semicoke as a product; and (3) further deeply processing and applying the coal gas and tar obtained after pyrolysis crude coal gas obtained by pyrolysis of the pea coal enters a crude coal gas treatment system, and carrying out gasification reaction on the obtained pyrolysis semicoke of the pea coal and air in a gasification system to generate gasified coal gas. The coal briquette pyrolysis furnace can process full-particle-size raw coal, can realize self-heating balance of system energy, and can play a role in removing dust for gasified and pyrolyzed coal gas by being used as a particle bed separator. However, the reaction system is complicated, and the heat carrier of lump coal pyrolysis, namely gasification gas, contains a large amount of N2And CO2Resulting in low gas calorific value; lump coal is used as a filter material, the dust removal efficiency is low, most of dust of coal gas cannot be collected, the coal gas output by a lump coal pyrolysis system is used as a heat carrier of a pea coal pyrolysis system and is finally discharged from the pea coal pyrolysis system, secondary entrainment of the dust can be caused, and the coal gas still contains a large amount of dust.
Patent CN201610872192.4 discloses a method and a device for preparing semi coke, tar and coal gas from coal. The method utilizes a device comprising a drying classifier, a pulverized coal gasification reactor, a riser combustion reactor and a lump coal pyrolysis reactor to dry and classify raw material coal with mixed granularity into pulverized coal and lump coal, the pulverized coal is partially gasified by water vapor and oxygen, flue gas generated by burning of gasified semicoke is used for drying and classifying the raw material coal, and unburned residual high-temperature semicoke is used as a circulating solid heat carrier for gasifying the pulverized coal; lump coal is pyrolyzed by using gasified coal gas generated by powder coal gasification as a gas heat carrier, and meanwhile, the lump coal and semi coke are used as filter materials of a moving particle bed to collect dust carried by the pulverized coal gasified gas. The method realizes the preparation of high-quality semi coke by using the mixed-granularity coal as a production raw material, has high utilization rate of the raw material, and solves the problem of low gas heat value in the existing semi coke production technology. But the pyrolysis reactor is also used as a dust remover to remove dust from the gasified coal gas, and the particle size of lump coal and semi coke is large, so that the dust removal efficiency is low, and the pyrolysis and gasification mixed coal gas containing dust directly enters the post-treatment unit without removing dust; the gasified coal gas carrying a large amount of dust is conveyed to the pyrolysis reactor through the external connecting pipe route by the gasification reactor, and the pipeline is easy to be blocked by tar and dust; the device is complicated in construction.
Disclosure of Invention
The invention provides a device and a method for preparing semi-coke from coal, aiming at the problems of low utilization rate of pulverized coal resources, low calorific value of coal gas, dust removal of coal gas, device composition and the like in the semi-coke preparation process.
The technical scheme of the invention is as follows:
the device for preparing semi-coke from coal mainly comprises a pulverized coal gasification unit 1, a lump coal pyrolysis unit 2, a coal gas dust removal unit 3 and accessory equipment, wherein the accessory equipment comprises a drying and grading unit 4, a pulverized coal storage tank 5, a lump coal storage tank 6, a flue gas heat exchanger 7, a flue gas dust remover 8, a coke quenching unit 9, a coal gas purification unit 10 and a filter material regeneration unit 11.
Wherein, the pulverized coal gasification unit 1 comprises a semicoke combustion chamber 12, a pulverized coal gasification chamber 13 and a settling chamber 14; the combustion chamber 12 is separated from the gasification chamber 13 by a baffle plate a 15; the settling chamber 14 is positioned at the upper parts of the combustion chamber 12 and the gasification chamber 13, the settling chamber 14 is communicated with the combustion chamber 12 through a settling pipe 16, and the settling chamber 14 is communicated with the gasification chamber 13; the bottom of the combustion chamber 12 is communicated with the bottom of the gasification chamber 13 through a material returning device 17 for circulating the semicoke and ash of the solid heat carrier; an air inlet 18 is arranged at the lower part of the combustion chamber 12, a flue gas outlet 19 is arranged at the side of the upper part of the combustion chamber 12, the flue gas outlet 19 is positioned above the free separation space of the combustion chamber 12 and below the settling chamber 14, and the flue gas outlet 19 is connected with the flue gas dust remover 8; the lower part of the gasification chamber 13 is provided with a pulverized coal inlet 20, a gasifying agent inlet 21 and an ash outlet 22 which are all positioned below the material returning device 17, and the pulverized coal inlet 20 is connected with the pulverized coal storage tank 5;
the lump coal pyrolysis unit 2 is positioned above the side of the pulverized coal gasification unit 1, the pulverized coal gasification unit 1 and the lump coal pyrolysis unit 2 are separated by a baffle b24 with a shutter a23 at the lower part, and the pulverized coal gasification unit 1 is communicated with the lump coal pyrolysis unit 2 through a gas flow channel formed by the shutter a 23; louvres a23 are located in the upper part of the settling chamber 14 with the lower end higher than the upper end of the baffle a 15; the main body of the lump coal pyrolysis unit 2 is a pyrolysis chamber 25, the top of the lump coal pyrolysis unit 2 is provided with a lump coal inlet 26, the bottom of the lump coal pyrolysis unit 2 is provided with a semi-coke outlet 27, wherein the lump coal inlet 26 is connected with the lump coal storage tank 6, and the semi-coke outlet 27 is connected with the coke quenching unit 9 through a discharge valve; the lump coal pyrolysis unit 2 and the coal gas dust removal unit 3 are separated by a baffle c28, an inner member 29 is arranged at the upper part of the baffle c28, and the lump coal pyrolysis unit 2 is communicated with the coal gas dust removal unit 3 through a gas flow channel formed by the inner member 29; the bottom end of the inner member 29 is higher than the top end of the shutter a23, so that the material in the pyrolysis chamber 25 forms a gas-solid countercurrent mode;
the main body of the coal gas dust removal unit 3 is a dust removal chamber 30, the top of the dust removal chamber 30 is provided with a filter material inlet 31, the bottom of the dust removal chamber 30 is provided with a filter material outlet 32, the filter material inlet 31 is connected with a filter material outlet of the filter material regeneration unit 11, and the filter material outlet 32 is connected with the filter material inlet of the filter material regeneration unit 11 through a discharge valve; the gas dust chamber 30 is provided with a gas outlet 33, and the position of the gas dust chamber has two setting modes: one is that the center of the inner component 29 is at the same horizontal height, the filter material is kept in the dust chamber 30 through the shutter b34, so that the gas in the dust chamber 30 and the filter material form a gas-solid cross flow mode; the other is arranged at the upper part of the coal gas dust chamber 30 and is positioned above the inner member 29, and the filter material is kept in the dust chamber 30 through a baffle d35, so that the coal gas and the filter material in the dust chamber 30 form a gas-solid countercurrent mode; the gas outlet 33 is connected with the gas purification unit 10;
in the accessory equipment, a drying and grading unit 4 is provided with a raw material coal inlet, a pulverized coal outlet, a lump coal outlet and a flue gas outlet which are respectively connected with a pulverized coal storage tank 5 and a lump coal storage tank 6; the drying and grading unit 4 is connected with the pulverized coal gasification unit 1, and a flue gas heat exchanger 7 and a flue gas dust remover 8 are arranged between the drying and grading unit and the pulverized coal gasification unit; the coke quenching unit 9 is provided with a coke quenching medium inlet, a coke quenching medium outlet and a semi coke outlet; the gas purification unit 10 is provided with a gas outlet, a tar outlet and a pyrolysis water outlet; the filter material regeneration unit 11 is provided with an air inlet, a fuel inlet, a supplementary filter material inlet and a flue gas outlet.
The flow cross sections of the combustion chamber 12, the gasification chamber 13, the pyrolysis chamber 25 and the dust removal chamber 30 are rectangular structures or circular structures;
the combustion chamber 12 and the gasification chamber 13 are bubbling fluidized beds;
the inner member 29 is a saddle-shaped louver structure or a wedge-shaped screen structure.
The method for preparing semi-coke by coal adopts the device for preparing semi-coke by coal, and comprises the following specific steps:
the raw material coal is input into a drying and grading unit 4, is dried and graded into pulverized coal and lump coal under the action of flue gas, and respectively enters a pulverized coal storage tank 5 and a lump coal storage tank 6; dry pulverized coal from the pulverized coal storage tank 5 enters the gasification chamber 13 of the pulverized coal gasification unit 1 through the pulverized coal inlet 20, and the dry pulverized coal is fluidized and subjected to gasification reaction under the action of a gasification agent input from the gasification agent inlet 21; the gasified gas and the semicoke enter a settling chamber 14 to generate gas-solid settling separation, wherein the gasified gas as a gas heat carrier for lump coal pyrolysis enters a pyrolysis chamber 25 of the lump coal pyrolysis unit 2 through a shutter a23, and the gasified semicoke falls into a semicoke combustion chamber 12 through a settling pipe 16; in the combustion chamber 12, the semicoke is fluidized by air input from an air inlet 18 and undergoes a partial combustion reaction to generate high-temperature flue gas, residual semicoke and ash, wherein the flue gas is output from a flue gas outlet 19, is sequentially subjected to dust removal by a flue gas dust remover 8 and cooling by a flue gas heat exchanger 7 and then is input into a drying and grading unit 4 of raw material coal as a drying and grading medium of the raw material coal, and the residual semicoke and ash are returned to the gasification chamber 13 through a return feeder 17 to serve as a circulating solid heat carrier for pulverized coal gasification. In the process of gasifying the pulverized coal, the gasified semicoke accumulated in the settling tube 16 and at the lower part of the settling chamber 14 and the pressure difference between the combustion chamber 12 and the gasification chamber 13 are utilized to isolate the combustion and the gas atmosphere at the upper parts of the combustion chamber 12 and the gasification chamber 13; the combustion and the gas atmosphere in the lower part of the combustion chamber 12 and the gasification chamber 13 are isolated by the ring seal assembly of the return feeder 17, and solid particles (gasification semicoke or combustion semicoke and ash) are circulated between the combustion chamber 12 and the gasification chamber 13 by the settling tube 16 and the return feeder 17.
Dried lump coal from the lump coal storage tank 6 enters the pyrolysis chamber 25 of lump coal through a lump coal inlet 26. The lump coal moves downwards under the action of gravity, is heated by gasification gas flowing reversely from the pulverized coal gasification unit 1 and generates pyrolysis reaction to generate raw coke and semi coke. Raw gas (including gasified gas and pyrolysis gas) goes upwards to pass through the semi-coke and lump coal bed, and part of dust carried by the raw gas is captured by the semi-coke and lump coal in the process. The primarily dedusted mixed gas of gasification and pyrolysis passes through the inner member 29 into the dedusting chamber 30 of the gas dedusting unit 3. High-temperature semi coke generated by pyrolysis is moved out from a semi coke outlet 27 under the control of a discharge valve and enters a coke quenching unit 9, and is output as a product after being swept and cooled by a coke quenching medium; meanwhile, small granular coke powder carried by the semi coke is taken out by a coke quenching medium;
in the gas clean room 30, the filter media from the media regeneration unit 11 descends under gravity to form a moving bed of particles. The mixed gas of gasification and pyrolysis entering from the lump coal pyrolysis unit 2 passes through the moving particle bed of the dust removal chamber 30 in a counter-current or radial cross-flow manner, and dust in the gas is further captured. The clean coal gas after dust removal is output from a coal gas outlet 33 and enters a coal gas purification unit 10, and the coal gas, tar and water are obtained after cooling and separation; the filter material after dust collection is moved out from the filter material outlet 32 under the control of the discharge valve and then enters the filter material regeneration unit 11. In the filter material regeneration unit 11, the carbon deposit on the filter material is burned off by air, and the filter material is heated by burning supplementary fuel (such as self-produced purified gas), and the dust carried by the filter material is removed by the burning flue gas, so that the filter material is regenerated. If necessary, fresh filter material is added to the filter material regeneration unit 11 to compensate for the loss of filter material due to crushing and pulverization during the circulation process. The regenerated filter material is separated from the combustion flue gas and then returns to the coal gas dust removal unit 3 through a filter material inlet 31;
all the operations are carried out under normal pressure. The gasification temperature of the pulverized coal is 800-1000 ℃, the retention time of the pulverized coal is 1-45 min, the gasifying agent is water and oxygen, the water-coal ratio is 0.2-0.7, the oxygen-coal ratio is 0.2-0.5, and the temperature of the gasifying agent is not lower than 400 ℃; the burning temperature of the semicoke is higher than the gasification temperature, the upper limit is lower than the melting point of the coal ash by 150 ℃, the temperature is generally not higher than 1200 ℃, and the temperature of air entering a combustion chamber is not lower than 400 ℃; the mass ratio of the circulating semicoke to the pulverized coal is not more than 50, and the preferable range is 1-10; the pyrolysis temperature of the lump coal is 500-800 ℃, and the retention time of the lump coal is 15-60 min; the mass ratio of the pulverized coal to the lump coal is 1.5: 1-8: 1, and under the selected feeding ratio, the heat carried by the pulverized coal gasified coal gas meets the energy requirement of lump coal pyrolysis.
The circulation rate of the filter material in the coal gas dust removal unit 3 is 0.8-5 m/h, and the temperature of the filter material is 400-650 ℃; the circulation rate and the temperature of the filter material can be independently regulated and controlled, so that the high-efficiency dust removal of coal gas with different temperatures, different tar contents and different dust contents under different semi-coke production conditions is met, and meanwhile, the accumulation of a filter material bed layer and the loss of tar caused by the condensation and coking of the tar are avoided;
the filter material is inert or solid particles with catalytic activity, and comprises one or more than two of ceramics, coal gangue, natural ore, charcoal, coal coke or catalysts;
the particle size range of the filter material is 0.1-15 mm, and the preferred particle size is 2-4 mm;
the raw material coal is low-rank coal such as brown coal, long flame coal, non-sticky coal or weakly sticky coal;
the granularity of the raw material coal is not more than 80mm, the upper limit of the granularity limit of the pulverized coal is not more than 13mm, the upper limit of the granularity limit of the further optimized pulverized coal is not more than 6mm, and the rest is lump coal, so that the pulverized coal and semicoke generated by gasification can be fluidized and lifted in a gasification chamber and a combustion chamber, the air permeability of bed materials during lump coal pyrolysis can be kept, and meanwhile, a moving particle layer formed by the lump coal and pyrolysis semi-coke has a certain trapping effect on dust carried by the gasified coal gas, and primary dust removal is formed;
the coke quenching medium is flue gas output by the drying and grading unit 4 or the filter material regeneration unit 11, and the flue gas produced by the utilization process as the coke quenching medium can not only realize the maximum utilization of materials and energy, but also improve the performance of semi coke and reduce the environmental pollution by adopting a dry coke quenching mode;
the method can be used for the decoupling thermal conversion process of solid fuel, and the preparation of synthesis gas, hydrogen-rich gas, methane-rich gas or high-quality tar is realized by adjusting the input positions and types of raw materials and filter materials to enable the pulverized coal gasification unit 1 or the pulverized coal gasification unit 1 and the lump coal pyrolysis unit 2 to be used as fuel units, and the lump coal pyrolysis unit 2 or the lump coal pyrolysis unit 2 and the coal gas dust removal unit 3 to be used as coal gas or tar catalytic upgrading units.
The invention has the beneficial effects that:
(1) the device comprises the gasification unit, the pyrolysis unit and the coal gas dust removal unit which are communicated only through the gas or solid flow channel, so that the gasification of pulverized coal, the pyrolysis of lump coal and the in-situ thermal dust removal of coal gas are integrated, and each unit is relatively independent in operation, and has the advantages of simple structure, strong processing capacity, strong adjustability, high comprehensive energy efficiency, small occupied area and stable operation;
(2) the method utilizes pulverized coal gasification semicoke as a circulating heat carrier for pulverized coal gasification, pulverized coal gasification gas as a heat carrier for preparing semi-coke by pyrolysis of lump coal, and simultaneously utilizes the lump coal pyrolysis unit as a movable particle dust removal unit to primarily remove dust from the pulverized coal gasification gas, and then utilizes the gas dust removal unit to carry out thermal high-temperature in-situ dust removal on the gasification and pyrolysis gas, thereby realizing the self-heating balance of energy and the self-purification of gas, and solving the key problems of low utilization rate of pulverized coal resources, high dust content of gas and low heat value of pyrolysis gas which restrict the semi-coke production;
(3) the lump coal pyrolysis unit and the coal gas dust removal unit are two-section coupled coal gas in-situ thermal dust removal, the operation modes are various, the moving speed of a filter material can be independently regulated, the dust removal pressure drop is small, the dust removal efficiency is high, the semi-coke production process is continuous and stable, and the comprehensive energy efficiency is high;
(4) the device and the method can be used for the decoupling thermal conversion process of solid fuel, and the types and input positions of raw materials and filter materials are adjusted, so that the pulverized coal gasification unit or the pulverized coal gasification unit and the lump coal pyrolysis unit are used as fuel units, and the lump coal pyrolysis unit or the lump coal pyrolysis unit and the coal gas dust removal unit are used as coal gas or tar catalytic upgrading units, thereby realizing the preparation of synthesis gas, hydrogen-rich, methane-rich or high-quality tar.
Drawings
FIG. 1 is a schematic diagram of the device composition and process flow for preparing semi-coke from coal.
FIG. 2 is a schematic diagram of the principle of the device in which the gas dust removal unit is in a cross-flow moving bed operation mode.
FIG. 3 is a schematic diagram of the principle of the device in which the gas dust removal unit is in a counter-current moving bed operation mode.
In the figure: 1 a pulverized coal gasification unit; 2 coal pyrolysis units; 3, a coal gas dust removal unit; 4, a drying and grading unit; 5, a pulverized coal storage tank; 6 coal storage tanks; 7, a flue gas heat exchanger; 8 flue gas dust remover; 9 a coke quenching unit; 10 gas purification unit; 11 a filter material regeneration unit; 12 a combustion chamber; 13 a gasification chamber; 14 a settling chamber; 15 baffle a; 16 a settling tube; 17 a material returning device; 18 an air inlet; 19 a flue gas outlet; 20, a pulverized coal inlet; 21 a gasifying agent inlet; 22 an ash outlet; 23 louver a; 24 baffle b; 25 a pyrolysis chamber; 26 coal inlets; 27 a semi-coke outlet; 28 baffle c; 29 inner member; 30, a dust removal chamber; 31 a filter material inlet; 32 a filter material outlet; 33 gas outlet; 34 louver b; 35 baffle d.
Detailed Description
The present invention will be further described with reference to the following technical solutions and the accompanying drawings, which are not intended to limit the scope of the present invention.
The device composition and the process flow for preparing semi-coke by coal are shown in figure 1.
Example 1
The operation principle of the apparatus adopted in this embodiment is shown in fig. 2, wherein the combustion chamber 12 and the gasification chamber 13 are bubbling fluidized beds, the pyrolysis chamber 25 is a counter-current moving bed, the dust removal chamber 30 is a cross-flow moving bed, and the flow cross section of each reaction chamber is a rectangular structure. The raw material coal with the particle size of less than 80mm passes through the drying and grading unit 4 and is dried and decomposed into pulverized coal with the moisture content of less than 10 percent and the particle size of less than 10mm and lump coal with the moisture content of less than 6 percent and the particle size of 10-80 mm under the condition that the combustion flue gas is taken as a drying medium, and the pulverized coal and the lump coal are respectively stored in the pulverized coal storage tank 5 and the lump coal storage tank 6. Dried pulverized coal from a pulverized coal storage tank 5 is conveyed to a gasification chamber 13 through a pulverized coal inlet 20 at a feeding rate of 0.60kg/h, water vapor and oxygen with the temperature of 400 ℃ are conveyed to the gasification chamber 13 through a gasifying agent inlet 21, the water-coal ratio is 0.2, the oxygen-coal ratio is 0.2, and then the pulverized coal is fluidized in the gasification chamber 13 with the temperature of 800 ℃ and normal pressure under the action of the water vapor and the oxygen and simultaneously gasification reaction occurs; the gasified semicoke and the coal gas enter a settling chamber 14 for gas-solid separation, the gasified semicoke falls into a semicoke combustion chamber 12 through a settling pipe 16, and the gasified coal gas enters a lump coal pyrolysis unit 2 through a shutter a 23. Air with the temperature of 400 ℃ is conveyed to the combustion chamber 12 through the air inlet 18 and is subjected to partial combustion reaction with the gasified semicoke, combustion products are separated in a free separation space at the upper part of the combustion chamber 12, flue gas with the temperature of 1000 ℃ passes through the flue gas outlet 19 output device, the output flue gas is dedusted by the flue gas deduster 8, enters the drying and grading unit 4 after being preheated by the flue gas heat exchanger 7, is output after being dried and graded for raw material coal, and then enters the coke quenching unit 9; the residual semicoke and ash content heated by combustion and having the temperature of 1000 ℃ are returned to the gasification chamber 13 through a return feeder 17 to be used as a circulating solid heat carrier for gasifying the pulverized coal, the mass ratio of the solid carrier to the pulverized coal is 8:1, and the accumulated ash content which cannot be fluidized and lifted is discharged out of the device through an ash content outlet 22; dry lump coal from the lump coal storage tank 6 enters the pyrolysis chamber 25 through the lump coal inlet 26 at a feeding rate of 0.4kg/h to form a moving particle bed of lump coal, and is in countercurrent contact with the gasification coal gas with the temperature of 800 ℃ entering the pulverized coal gasification unit 1 to generate pyrolysis reaction at the temperature of 500 ℃ under normal pressure; meanwhile, lump coal and semi coke are used as filter materials to carry out primary dust removal on the gasified coal gas. Semi coke generated by pyrolysis is moved out of the device from a semi coke outlet 27 under the control of a discharge valve and enters a coke quenching unit 9, and is output as a product after being cooled by dry flue gas and coke powder is removed, and a coke quenching medium is output from the device; the gasified and pyrolyzed gas passes through the inner member 29 of the shutter structure and enters the gas dust removing unit 3; quartz sand with the temperature of 500 ℃ and the temperature of 2-4 mm is used as a filter material and enters a coal gas dust removal chamber 30 through a filter material inlet 31 to form a dust removal particle bed, the quartz sand and pyrolysis coal gas with the temperature of 500 ℃ entering a lump coal pyrolysis unit 2 flow in a radial staggered manner to form a cross flow particle bed for dust removal, and the filter material for collecting dust is moved out of a device from a filter material outlet 32 and enters a filter material regeneration unit 11 at the moving speed of 0.8m/h under the control of a discharge valve. Meanwhile, the filter material regeneration unit 11 supplements fresh filter materials with proper quality, and the fresh filter materials are subjected to decarburization, preheating and dust removal under the combustion heat of input air and self-produced gas and then are used as circulating filter materials to return to the gas dust removal unit 3 and the flue gas output device; the clean coal gas of the coal gas dust removal unit 3 passes through the shutter b34 and is output from the coal gas outlet 33, the output coal gas enters the coal gas purification unit 10, and the coal gas, the tar and the pyrolysis water are obtained after cooling and separation.
Example 2
The operation principle of the apparatus used in this embodiment is shown in fig. 3, in which the combustion chamber 12 and the gasification chamber 13 are bubbling fluidized beds, the pyrolysis chamber 25 is a counter-current moving bed, the dust removal chamber 30 is a counter-current moving bed, and the cross-section of each reaction chamber is a circular structure. Different from the example 1, the particle size of the pulverized coal is less than 13mm, the feeding rate of the pulverized coal is 0.90kg/h, the temperature of the gasification chamber 13 is 900 ℃, the mass ratio of the solid circulating semicoke to the pulverized coal is 10:1, and the oxygen-coal ratio is 0.5; the particle size of the lump coal is 13-80 mm, the feeding rate of the lump coal is 0.15kg/h, and the temperature of the lump coal pyrolysis unit 2 is 750 ℃. The filter material is an olivine catalyst with the particle size of 3-5 mm and the temperature of 450 ℃, the olivine catalyst and pyrolysis gas flow reversely in the coal gas dust removal unit 3 to form a countercurrent particle layer for dust removal, the filter material is output at the moving speed of 1.0m/h, and clean coal gas is separated from the filter material at a gas-solid separation interface of the dust removal chamber 30 and then is output from the coal gas outlet 33 to enter the coal gas purification unit.
Example 3
The operation principle of the apparatus used in this embodiment is shown in fig. 2, in which the combustion chamber 12 and the gasification chamber 13 are bubbling fluidized beds, the pyrolysis chamber 25 is a counter-current moving bed, the dust removal chamber 30 is a cross-flow moving bed, and the flow cross section of each reaction chamber is a circular structure. Different from the example 1, the particle size of the pulverized coal is less than 10mm, the feeding rate of the pulverized coal is 0.80kg/h, the temperature of the gasification chamber 13 is 800 ℃, the mass ratio of the solid circulating semicoke to the pulverized coal is 15:1, the water-coal ratio is 0.7, and the oxygen-coal ratio is 0.2; the particle size of the lump coal is 10-50 mm, the feeding rate of the lump coal is 0.10kg/h, and the pyrolysis temperature is 650 ℃. The filter material is 1-2 mm quartz sand with the temperature of 400 ℃, and the filter material is output to the coal gas dust removal unit 3 at the moving speed of 5 m/h.
Example 4
The operation principle of the apparatus used in this embodiment is shown in fig. 3, in which the combustion chamber 12 and the gasification chamber 13 are bubbling fluidized bed beds, the pyrolysis chamber 25 is a counter-current moving bed, the dust removal chamber 30 is a counter-current moving bed, and the cross-section of each reaction chamber is rectangular. Different from the example 2, the particle size of the pulverized coal is less than 10mm, the feeding rate of the pulverized coal is 1.00kg/h, the temperature of the gasification chamber 13 is 1000 ℃, the temperature of the semicoke combustion chamber is 1100 ℃, the mass ratio of the solid circulating semicoke to the pulverized coal is 12:1, the water-coal ratio is 0.2, and the oxygen-coal ratio is 0.4; the particle size of the lump coal is 10-80 mm, the feeding rate of the lump coal is 0.5kg/h, and the pyrolysis temperature is 800 ℃. The filter material is quartz sand with the particle size of 2-6 mm and the temperature of 650 ℃, and the filter material is a coal gas dust removal unit 3 with the moving speed of 1.2 m/h.
Example 5
The operation principle of the device adopted in the embodiment is shown in figure 2, the combustion chamber 12 and the gasification chamber 13 are bubbling fluidized beds, the lump coal pyrolysis chamber 25 is a counter-current moving bed, the coal gas dust removal chamber 30 is a cross-flow moving bed, and the flow cross section of each reaction chamber is of a circular structure. The raw material coal with the particle size of less than 60mm is dried and classified into pulverized coal with the moisture content of less than 12 percent and the particle size of less than 13mm and lump coal with the moisture content of less than 8 percent and the particle size of 13-80 mm by combustion flue gas in the drying and classifying unit 4. The pulverized coal enters the gasification chamber 13 from a pulverized coal inlet 20 at a feeding rate of 0.50kg/h, water vapor and oxygen with the water-coal ratio of 0.5 and the oxygen-coal ratio of 0.4 at the temperature of 400 ℃ enter the gasification chamber 13 from a gasification test inlet 21, and the pulverized coal is gasified at 950 ℃ and normal pressure under the heating of fluidization and circulating semicoke of a gasification agent. The gasified semicoke and the gasified coal gas are subjected to gas-solid separation in the settling chamber 14, the gasified semicoke falls into the semicoke combustion chamber 12 through the settling pipe 16, and the gasified coal gas enters the lump coal pyrolysis unit 2 through the shutter a 15. Air with the temperature of 400 ℃ enters the combustion chamber 12 from the air inlet 18, contacts with the gasified semicoke to perform partial combustion reaction, the combustion temperature is 1050 ℃, the flue gas generated by combustion is separated from high-temperature solids in the free separation space at the upper part of the combustion chamber 12 and then is output through the flue gas outlet 19, and the flue gas sequentially passes through the flue gas dust remover 8 and the flue gas heat exchanger 7 and then is used as a drying medium of the drying and grading unit 4; the semicoke and the ash content which are heated by combustion are returned to the gasification chamber 13 through a return feeder 17 to be used as a circulating solid heat carrier for gasifying the pulverized coal, the mass ratio of the solid carrier to the pulverized coal is 10:1, and the accumulated ash content which can not be lifted and fluidized is discharged out of the device through an ash content outlet 22; lump coal enters the lump coal pyrolysis chamber 25 from the lump coal inlet 26 at a feed rate of 0.3kg/h to form a lump coal particle bed, and is in countercurrent contact with gasification coal gas entering the pulverized coal gasification unit 1 to perform pyrolysis reaction at 700 ℃ under normal pressure. Meanwhile, lump coal and semi coke are used as filter materials to carry out preliminary dust removal on the gasified gas, and the dedusted gasified gas and the pyrolyzed mixed gas pass through the inner member 29 of the shutter structure and enter the gas dust removal unit 3; semi coke generated by pyrolysis is moved out of the device under the control of a discharge valve and enters a coke quenching unit 9, and the semi coke with the particle size larger than 6mm after being quenched, dedusted and classified by dry flue gas is output as a product; semi coke with the particle size not more than 6mm enters a filter material regeneration unit 11, after semi coke with proper mass and the same particle size is supplemented, the semi coke and the gasified coal gas are combusted at the temperature of 450 ℃, the semi coke and the gasified coal gas are preheated and deashed and then return to a coal gas dust removal chamber 30 through a filter material inlet 31 to form a dust removal particle bed, and the semi coke and the lump coal pyrolysis unit 2 enter pyrolysis coal gas to flow in a radial staggered manner to form a cross flow particle bed for dust removal, and the semi coke for collecting dust is circulated back to the filter material regeneration unit 11 from a filter material outlet 32 at the moving speed of 1.5m/h under the control of; the clean coal gas passes through the shutter b34 and is output from the coal gas outlet 33 to enter the coal gas purification unit 10, and the coal gas, the tar and the water are obtained after cooling and separation.
TABLE 1 composition of raw coal in examples
Differential subtraction
TABLE 2 analysis of the products of the examples
Claims (10)
1. The device for preparing the semi-coke by the coal is characterized by mainly comprising a pulverized coal gasification unit (1), a lump coal pyrolysis unit (2), a coal gas dust removal unit (3) and accessory equipment, wherein the accessory equipment comprises a drying and grading unit (4), a pulverized coal storage tank (5), a lump coal storage tank (6), a flue gas heat exchanger (7), a flue gas dust remover (8), a coke quenching unit (9), a coal gas purification unit (10) and a filter material regeneration unit (11);
wherein the pulverized coal gasification unit (1) comprises a semicoke combustion chamber (12), a pulverized coal gasification chamber (13) and a settling chamber (14); the combustion chamber (12) is separated from the gasification chamber (13) by a baffle plate a (15); the settling chamber (14) is positioned at the upper parts of the combustion chamber (12) and the gasification chamber (13), the settling chamber (14) is communicated with the combustion chamber (12) through a settling pipe (16), and the settling chamber (14) is communicated with the gasification chamber (13); the bottom of the combustion chamber (12) is communicated with the bottom of the gasification chamber (13) through a material returning device (17) for circulating solid heat carrier semi-coke and ash; an air inlet (18) is arranged at the lower part of the combustion chamber (12), a flue gas outlet (19) is arranged at the side of the upper part of the combustion chamber (12), the flue gas outlet (19) is positioned above the free separation space of the combustion chamber (12) and below the settling chamber (14), and the flue gas outlet (19) is connected with a flue gas dust remover (8); the lower part of the gasification chamber (13) is provided with a pulverized coal inlet (20), a gasifying agent inlet (21) and an ash outlet (22) which are all positioned below the material returning device (17), and the pulverized coal inlet (20) is connected with the pulverized coal storage tank (5);
the lump coal pyrolysis unit (2) is positioned above the side of the pulverized coal gasification unit (1), the pulverized coal gasification unit and the lump coal pyrolysis unit are separated by a baffle b (24) with a shutter a (23) at the lower part, and the pulverized coal gasification unit (1) is communicated with the lump coal pyrolysis unit (2) through a gas flow channel formed by the shutter a (23); the shutter a (23) is positioned at the upper part of the settling chamber (14), and the bottom end of the shutter a (23) is higher than the top end of the baffle a (15); the main body of the lump coal pyrolysis unit (2) is a pyrolysis chamber (25), the top of the lump coal pyrolysis unit (2) is provided with a lump coal inlet (26), the bottom of the lump coal pyrolysis unit is provided with a semi-coke outlet (27), wherein the lump coal inlet (26) is connected with the lump coal storage tank (6), and the semi-coke outlet (27) is connected with the coke quenching unit (9) through a discharge valve; the lump coal pyrolysis unit (2) and the coal gas dust removal unit (3) are separated by a baffle plate c (28), an inner member (29) is arranged at the upper part of the baffle plate c (28), and the lump coal pyrolysis unit (2) is communicated with the coal gas dust removal unit (3) through a gas flow channel formed by the inner member (29); the bottom end of the inner member (29) is higher than the top end of the shutter a (23), so that the materials in the pyrolysis chamber (25) form a gas-solid countercurrent mode;
the main body of the coal gas dust removal unit (3) is a dust removal chamber (30), the top of the coal gas dust removal unit (3) is provided with a filter material inlet (31), the bottom of the coal gas dust removal unit (3) is provided with a filter material outlet (32), the filter material inlet (31) is connected with the filter material outlet of the filter material regeneration unit (11), and the filter material outlet (32) is connected with the filter material inlet of the filter material regeneration unit (11) through a discharge valve; the dust chamber (30) is provided with a coal gas outlet (33), and the position of the dust chamber has two setting modes: one is that the center of the inner component (29) is at the same horizontal height, the filter material is kept in the dust chamber (30) through the shutter b (34), so that the gas in the dust chamber (30) and the filter material form a gas-solid cross flow mode; the other is arranged at the upper part of the dust chamber (30) and positioned above the inner member (29), and the filter material is kept in the dust chamber (30) through a baffle d (35), so that the gas and the filter material in the dust chamber (30) form a gas-solid countercurrent mode; the gas outlet (33) is connected with the gas purification unit (10);
in the accessory equipment, a drying and grading unit (4) is provided with a raw material coal inlet, a pulverized coal outlet, a lump coal outlet and a flue gas outlet which are respectively connected with a pulverized coal storage tank (5) and a lump coal storage tank (6); the drying and grading unit (4) is connected with the pulverized coal gasification unit (1), and a flue gas heat exchanger (7) and a flue gas dust remover (8) are arranged between the drying and grading unit and the pulverized coal gasification unit; the coke quenching unit (9) is provided with a coke quenching medium inlet, a coke quenching medium outlet and a semi-coke outlet; the coal gas purification unit (10) is provided with a coal gas outlet, a tar outlet and a pyrolysis water outlet; the filter material regeneration unit (11) is provided with an air inlet, a fuel inlet, a supplementary filter material inlet and a smoke outlet.
2. The apparatus for preparing semi-coke from coal according to claim 1, wherein the combustion chamber (12), the gasification chamber (13), the pyrolysis chamber (25) and the dust removal chamber (30) have a rectangular or circular cross-section.
3. The apparatus for preparing semi-coke from coal according to claim 1 or 2, wherein the combustion chamber (12) and the gasification chamber (13) are bubbling fluidized beds.
4. The apparatus for semi-coke preparation from coal according to claim 1 or 2, characterized in that the inner member (29) is a saddle-shaped louver structure or a wedge-shaped screen structure.
5. The method for preparing semi-coke by coal is characterized in that the device for preparing semi-coke by coal according to any one of claims 1 to 4 comprises the following steps:
the raw material coal is input into a drying and grading unit (4), is dried and graded into pulverized coal and lump coal under the action of flue gas, and respectively enters a pulverized coal storage tank (5) and a lump coal storage tank (6); dry pulverized coal from a pulverized coal storage tank (5) enters a gasification chamber (13) of a pulverized coal gasification unit (1) through a pulverized coal inlet (20), and the dry pulverized coal is fluidized and subjected to gasification reaction under the action of a gasification agent input from a gasification agent inlet (21); the gasified gas and the semicoke enter a settling chamber (14) to generate gas-solid settling separation, wherein the gasified gas as a gas heat carrier for lump coal pyrolysis passes through a shutter a (23) and enters a pyrolysis chamber (25) of a lump coal pyrolysis unit (2), and the gasified semicoke falls into a semicoke combustion chamber (12) through a settling pipe (16); in a semicoke combustion chamber (12), semicoke is fluidized by air input from an air inlet (18) and is subjected to partial combustion reaction to generate high-temperature flue gas, residual semicoke and ash, wherein the flue gas is output from a flue gas outlet (19), is used as a drying and classifying medium of raw material coal after being dedusted by a flue gas deduster (8) and cooled by a flue gas heat exchanger (7) and is input into a drying and classifying unit (4) of the raw material coal, and the residual semicoke and the ash are returned to a gasification chamber (13) through a return feeder (17) and are used as a circulating solid heat carrier for gasifying pulverized coal;
dry lump coal from the lump coal storage tank (6) enters a pyrolysis chamber (25) of the lump coal from a lump coal inlet (26); the lump coal moves downwards under the action of gravity, is heated by gasification gas flowing reversely from the pulverized coal gasification unit (1) and generates pyrolysis reaction to generate raw coke and semi coke; raw gas goes upwards to pass through the semi-coke and lump coal layer, and part of dust carried by the raw gas is trapped by the semi-coke and lump coal; the crude gas subjected to primary dust removal passes through the inner component (29) and enters a dust removal chamber (30) of the gas dust removal unit (3); high-temperature semi coke generated by pyrolysis is moved out from a semi coke outlet (27) under the control of a discharge valve and enters a coke quenching unit (9), and is output as a product after being swept and cooled by a coke quenching medium; meanwhile, small granular coke powder carried by the semi coke is taken out by a coke quenching medium;
in a dust chamber (30) of the coal gas, filter materials from a filter material regeneration unit (11) descend under the action of gravity to form a moving particle bed; raw gas entering from the lump coal pyrolysis unit (2) passes through a moving particle bed of the dust removal chamber (30) in a counter-current or radial cross-flow mode, and dust in the gas is further captured; the clean coal gas after dust removal is output from a coal gas outlet (33) and enters a coal gas purification unit (10), and the coal gas, tar and water are obtained after cooling and separation; the filter material after dust collection is moved out from a filter material outlet (32) under the control of a discharge valve and then enters a filter material regeneration unit (11); in the filter material regeneration unit (11), carbon deposit on the filter material is burnt out by air, the filter material is heated by the combustion of supplementary fuel, and dust carried by the filter material is removed by utilizing combustion flue gas to regenerate the filter material; according to actual needs, fresh filter materials are added in the filter material regeneration unit (11) to make up for the loss of the filter materials caused by crushing and pulverization in the circulation process; the regenerated filter material is separated from the combustion flue gas and then returns to the coal gas dust removal unit (3) through a filter material inlet (31);
the operation pressure is normal pressure; the gasification temperature of the pulverized coal is 800-1000 ℃, the retention time of the pulverized coal is 1-45 min, the gasifying agent is water and oxygen, the water-coal ratio is 0.2-0.7, the oxygen-coal ratio is 0.2-0.5, and the temperature of the gasifying agent is not lower than 400 ℃; the burning temperature of the semicoke is higher than the gasification temperature, the upper limit is lower than the melting point of the coal ash by 150 ℃ and is not higher than 1200 ℃, the temperature of air entering a combustion chamber is not lower than 400 ℃, and the mass ratio of the circulating semicoke to the pulverized coal is not more than 50; the pyrolysis temperature of the lump coal is 500-800 ℃, the retention time of the lump coal is 15-60 min, and the mass ratio of the pulverized coal to the lump coal is 1.5: 1-8: 1.
6. The method for preparing semi-coke by coal according to claim 5, wherein the circulation rate of the filter material in the coal gas dust removal unit (3) is 0.8-5 m/h, and the temperature of the filter material is 400-650 ℃.
7. The method for preparing semi-coke by using coal as claimed in claim 5 or 6, wherein the filter material is inert or solid particles with catalytic activity, and is one or a mixture of more than two of ceramics, natural ores or catalysts; the particle size range of the filter material is 0.1-15 mm.
8. The method for preparing semi-coke from coal according to claim 5 or 6, wherein the raw material coal is lignite, long-flame coal, non-sticky coal or weakly sticky coal, and the particle size is not more than 80 mm; the granularity of the pulverized coal is not more than 13mm, and the rest is lump coal.
9. The method for preparing semi-coke by coal according to claim 5 or 6, wherein the quenching medium is flue gas output by a dry classification unit (4) or a filter material regeneration unit (11).
10. The method for preparing semi-coke from coal according to claim 5 or 6, wherein the method is used for a decoupling thermal conversion process of solid fuel, the pulverized coal gasification unit (1) or the pulverized coal gasification unit (1) and the lump coal pyrolysis unit (2) are used as fuel units, and the lump coal pyrolysis unit (2) or the lump coal pyrolysis unit (2) and the coal gas dust removal unit (3) are used as coal gas or tar catalytic upgrading units, so that the preparation of synthesis gas, hydrogen-rich, methane-rich or high-quality tar is realized.
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